Classifications

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  • C01G41/00—Compounds of tungsten
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  • C01G41/00—Compounds of tungsten
  • C01G41/006—Compounds containing, besides tungsten, two or more other elements, with the exception of oxygen or hydrogen
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  • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
  • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
  • B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
  • B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
  • B01J23/85—Chromium, molybdenum or tungsten
  • B01J23/888—Tungsten
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  • B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
  • B01J27/14—Phosphorus; Compounds thereof
  • B01J27/186—Phosphorus; Compounds thereof with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
  • B01J27/188—Phosphorus; Compounds thereof with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium with chromium, molybdenum, tungsten or polonium
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  • B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
  • B01J27/14—Phosphorus; Compounds thereof
  • B01J27/186—Phosphorus; Compounds thereof with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
  • B01J27/188—Phosphorus; Compounds thereof with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium with chromium, molybdenum, tungsten or polonium
  • B01J27/19—Molybdenum
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  • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
  • B01J37/02—Impregnation, coating or precipitation
  • B01J37/0201—Impregnation
  • B01J37/0213—Preparation of the impregnating solution
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
  • B01J37/30—Ion-exchange
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  • C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
  • C01G53/00—Compounds of nickel
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  • C01—INORGANIC CHEMISTRY
  • C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
  • C01G53/00—Compounds of nickel
  • C01G53/006—Compounds containing, besides nickel, two or more other elements, with the exception of oxygen or hydrogen
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
  • C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
  • C10G45/04—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used
  • C10G45/06—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof
  • C10G45/08—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
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  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
  • C10G47/02—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used
  • C10G47/10—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used with catalysts deposited on a carrier
  • C10G47/12—Inorganic carriers
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G49/00—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00
  • C10G49/02—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00 characterised by the catalyst used
  • C10G49/04—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00 characterised by the catalyst used containing nickel, cobalt, chromium, molybdenum, or tungsten metals, or compounds thereof
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2523/00—Constitutive chemical elements of heterogeneous catalysts
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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  • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
  • B01J37/20—Sulfiding
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  • C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
  • C01P2002/00—Crystal-structural characteristics
  • C01P2002/80—Crystal-structural characteristics defined by measured data other than those specified in group C01P2002/70
  • C01P2002/82—Crystal-structural characteristics defined by measured data other than those specified in group C01P2002/70 by IR- or Raman-data
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  • C01P2002/80—Crystal-structural characteristics defined by measured data other than those specified in group C01P2002/70
  • C01P2002/86—Crystal-structural characteristics defined by measured data other than those specified in group C01P2002/70 by NMR- or ESR-data

Definitions

• the present invention describes a heteropolycomposed consisting of a nickel salt of a heteropolyanion of Keggin type lacunar comprising in its structure tungsten of formula
• Ni nickel
• A is selected from phosphorus, silicon and boron
• W is tungsten
• O oxygen
• x 4 if A is silicon
• z is a number between 0 and 36 and m is equal to 3 if A is phosphorus
• m is equal to 4 if A is silicon and m is equal to 5 if A is boron
• said heteropoly compound has no Nickel atom in substitution for a tungsten atom in its structure, said nickel atoms being placed in the counter ion position in the structure of said compound.
• the present invention also describes a process for preparing said heteropolycomposed consisting of a keggin lacunar type heteropolyanion nickel salt comprising in its structure tungsten.
• the present invention also relates to a catalyst comprising said heteropolycomposé and hydrocracking, hydroconversion and / or hydrotreatment processes using said catalysts.
• the invention relates to the hydrocracking of hydrocarbonaceous feeds containing, for example, aromatic and / or olefinic and / or naphthenic and / or paraffinic compounds including feedstocks resulting from the Fischer-Tropsch process and optionally containing metals. and / or nitrogen, and / or oxygen and / or sulfur.
• the objective of the hydrocracking process is essentially the production of middle distillates, ie cuts with initial boiling point of at least 150 ° C. and final up to the boiling point. initial residue, for example less than 340 0 C 1 or 370 0 C.
• the invention also relates to the hydrotreatment of hydrocarbon feedstocks such as petroleum cuts, cuts from coal or hydrocarbons produced from natural gas.
• hydrocarbon feedstocks comprise nitrogen and / or sulfur and / or aromatic and / or olefinic and / or naphthenic and / or paraffinic compounds, said feeds possibly containing metals and / or oxygen and / or sulfur.
• hydrotreating is meant the hydrogenation, hydrodesulphurization, hydrodenitrogenation, hydrodeoxygenation, hydrodearomatization and hydrodemetallation reactions.
• Hydrocracking of heavy oil cuts is a very important refining process which makes it possible to produce lighter fractions such as gasolines, jet fuels and light gas oils, which are sought by the refiner, from excessively heavy and undervalued feedstocks. to adapt its production to the structure of demand.
• Certain hydrocracking processes also make it possible to obtain a highly purified residue that can provide excellent bases for oils.
• the advantage of catalytic hydrocracking is to provide middle distillates, jet fuels and gas oils, of very good quality.
• the gasoline produced has a much lower octane number than that resulting from catalytic cracking.
• Hydrocracking is a process which derives its flexibility from three main elements which are the operating conditions used, the types of catalysts employed and the fact that the hydrocracking of hydrocarbon feeds can be carried out in one or two stages.
• the hydrocracking catalysts used in the hydrocracking processes are all of the bifunctional type associating an acid function with a hydro-dehydrogenating function.
• the acid function is provided by supports whose surfaces generally vary from 150 to 800 m 2 .g -1 and having a surface acidity, such as halogenated aluminas (chlorinated or fluorinated in particular), the combinations of boron oxides and aluminum, amorphous mesoporous aluminosilicates and zeolites.
• the hydro-dehydrogenating function is provided either by one or more metals of group VIB of the periodic table elements, either by a combination of at least one Group VIB metal of the Periodic Table with at least one Group VIII metal.
• the balance between the two acid and hydro-dehydrogenating functions is one of the parameters that governs the activity and the selectivity of the catalyst.
• a weak acid function and a strong hydro-dehydrogenating function give low active catalysts, working at a generally high temperature (greater than or equal to 390-400 ° C) and with a low feed-in space velocity (the WH expressed in volume charge to be treated per unit volume of catalyst per hour is generally less than or equal to 2), but with a very good selectivity in middle distillates (jet fuels and gas oils).
• a strong acid function and a low hydro-dehydrogenating function give active catalysts, but with lower selectivities in middle distillates.
• One type of conventional hydrocracking catalyst is based on moderately acidic amorphous supports, such as aluminosilicates for example. These systems are used to produce middle distillates of good quality, and possibly, oil bases. These catalysts are for example used in two-step processes.
• HDN hydrodearomatization
• HDS hydrodesulfurization
• NiW pair is recognized as the optimum group VIB and VIII metal pair for the hydrogenation of aromatics as well as for hydrodenitrogenation, key functions for hydrocracking.
• the NiW pair is recognized as the optimum group VIB and VIII metal pair for the hydrogenation of aromatics as well as for hydrodenitrogenation, key functions for hydrocracking.
• One of the scientific challenges of recent years is to optimize the hydrogenation phase deposited on various supports of catalysts for hydrocracking.
• the Applicant has unexpectedly demonstrated that the preparation of NiW type oxides from the nickel salt of a keggin-type heteropolyanion containing tungsten deposited on amorphous supports moderately Acids, such as aluminosilicate-type supports, have an advantage in terms of hydrogenating power: the catalysts thus prepared have improved catalytic performance in hydrocracking processes. It has thus surprisingly found that the use of the heteropoly compound of formula Ni ⁇ + y / 2 AWii -y ⁇ 39 .
• the present invention relates to a process for the preparation of said Ni salts of keggin-type heteropolyanions comprising W and their use during the preparation of catalysts. These heteropolyanions are highlighted by different physicochemical techniques.
• the richness of the tungsten chemistry allows the preparation of heteropolytungstite species more or less substituted and composed of the elements to be deposited. They are therefore chemical units whose degree of condensation of tungsten octahedra is controlled and where nickel is intimately related to the structure. These new materials used for the preparation of the impregnation solutions of the silica alumina support, will remove the 3 locks previously stated. Indeed the use of nickel salts of these heteropolanions will prevent the presence of ammonium ions known to be at the origin of the limit of good dispersion of the species, high metal content.
• heteropolyanions have already been mentioned in the state of the art.
• US Pat. No. 2,547,380 mentions the beneficial use of heteropoly acid salts of Group VIII metals such as the cobalt or nickel salts of phosphomolybdic acid or of silicomolybdic acid.
• the heteropoly acid always contains phosphorus or silicon, the latter being the central atom of the structure.
• These compounds have the disadvantage of leading to limited atomic ratios (Group VIII element / Group VI element).
• cobalt phosphomolybdate of formula has a Co / Mo ratio of 0.125.
• This increase of the ratio is obtained thanks to the presence of at least a part of the molybdenum or tungsten at a valence lower than its normal value of six as it results from the composition, for example, phosphomolybdic acid, phosphotungstic , silicomolybdic or silicotungstic.
• Patent application FR-A-2764211 describes the synthesis and use of heteropoly anions of the formula M x AB 11 O 40 M 1 C (Z. ⁇ Wherein M is cobalt or nickel, A is phosphorus, silicon or boron and B is molybdenum or tungsten, M 1 is cobalt, iron, nickel, copper or zinc, and C is an H + ion or an alkylammonium cation, x is O at 4.5, z a value between 7 and 9.
• this formula corresponds to that claimed in the invention FR-A-2, 749,778 but in which an atom M 1 is substituted for a B atom.
• the compounds are less soluble, iso support, it is not possible depositing as many precursors in a single impregnation with the compounds of FR-A-2,764,211 as with the compounds of the present invention.
• the hydrogenating activity being directly related to the amount of active phase deposited,
• An advantage of the present invention lies in the synthesis of these new heteropolycomposés and in the originality of their method of obtaining to obtain these compounds with high Ni / W ratio with a yield of more than 80%.
• the present invention discloses a heteropoly compound consisting of a nickel salt of a lacunar Keggin type heteropolyanion comprising in its structure tungsten of formula NUy / aAWn-yCWy, ZH 2 O (I)
• Ni nickel
• A is selected from phosphorus, silicon and boron
• W is tungsten
• O oxygen
• x 4 if A is silicon
• z is a number between 0 and 36 and m is equal to 3 if A is phosphorus
• m is equal to 4 if A is silicon and m is equal to 5 if A is boron
• said heteropoly compound has no Nickel atom in substitution for a tungsten atom in its structure, said nickel atoms being placed in the counter ion position in the structure of said compound.
• said heteropolycomposés do not have any nickel atom in substitution for a tunsgtenene atom.
• Nickel atoms are systematically placed in the counterion position in the structure and this, advantageously through the mode of preparation.
• the heteropolycomposed consisting of a nickel salt of a Keggin-type heteropolyanion comprising in its structure tungsten has the following formula
• A is a group chosen from phosphorus, silicon and boron
• W is tungsten
• O oxygen
• x is a number equal to 3.5 if the group A is phosphorus
• 4 if the group A is silicon or equal to 4.5 if the group A is the bor
• z is a number between 0 and 36, wherein said heteropolycomposé does not have any nickel atom in substitution for a tungsten atom in its structure, said nickel atoms being placed in the counterion position in the structure of said compound.
• said heteropolycomposé is the compound of formula: Ni 4 SiWnO 39 .
• the heteropolycomposed consisting of a nickel salt of a lacunar Keggin-type heteropolyanion comprising in its tungsten structure has the following formula:
• A is a group chosen from phosphorus, silicon and boron
• W is tungsten
• O oxygen
• x is a number equal to 3.5 if the group A is phosphorus, equal to 4 if the group A is silicon or equal to 4.5 if the group A is boron
• z is a number between
• heteropolycomposé has no Nickel atoms in substitution for a tungsten atom in its structure, said Nickel atoms being placed in the counter ion position in the structure of said compound.
• said heteropoly compound is the compound of formula Ni 5 SiW 9 O 34
• Said heteropolycomposés according to the invention are advantageously soluble in an aqueous medium. They are advantageously isolated and analyzed.
• the heteropolycomposés of formula (I) can advantageously be analyzed in solid form or in solution.
• 31 P NMR analyzes (nuclear magnetic resonance of P), by 29 Si NMR (Si nuclear magnetic resonance), and by 11 B NMR (B nuclear magnetic resonance) of heteropoly compounds of formula (I) do not reveal no transition between 300 and 600 ppm.
• a transition to such a chemical shift would be the sign that the paramagnetic nickel would have entered the structure in substitution of a tungsten atom, which is not the case of the heteropolycomposés according to the invention.
• the use of aqueous solutions of said heteropoly compounds for impregnating acidic porous supports, and preferably an acidic porous mineral matrix, and preferably aluminosilicate or zeolite type matrices diluted in alumina, has advantageously led to hydrocracking having increased hydrogenating activity.
• the present invention therefore also relates to a catalyst comprising said heteropolycomposed and optionally at least one porous acidic mineral matrix.
• One of the essential characteristics of the catalysts targeted by the present invention is the presence, at least in part, of said nickel and tungsten elements in the form of a heteropolycomposed according to the invention.
• the catalyst is in mass form.
• it advantageously contains, in the dried state, in% by weight relative to the total mass of the catalyst, from 0.01 to 100%, preferably from 0.05 to 100% and even more preferably from 0.1 to 100% of at least said heteropolycomposed according to the invention including at least nickel and at least tungsten and having a structure of (I) described above.
• said catalyst is a supported catalyst, the support being formed of at least one acid porous, preferably amorphous or poorly crystallized, mineral matrix chosen from mesostructured silica aluminosilicates, crystallized aluminosilicates or otherwise; or not, the doped aluminas (B, F, P), from the group formed by the family of crystallized non-zeolitic molecular sieves such as mesoporous silicas, silicalite, silicoaluminophosphates, aluminophosphates, ferrosilicates, titanium silicoaluminates, transition metal borosilicates, chromosilicates and aluminophosphates (including cobalt)
• the acidic porous mineral matrix may also advantageously contain, in addition to at least one of the abovementioned compounds, at least one synthetic or natural simple clay of 2: 1 dioctahedral phyllosilicate or 3: 1 trioctahedral phyllosilicate type, such as kaolinite, antigorite, chrysotile, montmorillonnite, beidellite, vermiculite, talc, hectorite, saponite, laponite. These clays can be optionally delaminated. It is also advantageous to use silica-alumina and clay mixtures.
• the matrix may also advantageously contain, in addition to at least one of the compounds mentioned above, at least one compound chosen from the group formed by the family of crystallized aluminosilicate molecular sieves, synthetic and natural zeolites such as zeolite Y fluorinated Y zeolite, zeolite Y containing rare earths, zeolite X, zeolite L, small pore mordenite, large pore mordenite, omega zeolites, NU-10, ZSM-5, ZSM-48, ZSM-22, ZSM-23, ZBM-30, EU-1, EU-2, EU-11, Beta, zeolite A, NU-87, NU- 88, NU-86, NU-85, IM-5, IM-12, IZM-2 and Ferrierite.
• synthetic and natural zeolites such as zeolite Y fluorinated Y zeolite, zeolite Y containing rare earths, zeolite X, zeolite L, small pore mor
• zeolites having a silicon / aluminum framework ratio (Si / Al) of greater than about 3: 1.
• Zeolites of faujasite structure and in particular stabilized and ultrastabilized Y zeolites (USY) are advantageously employed either in form at least partially exchanged with metal cations, for example alkaline earth metal cations and / or cations of earth metals. rare of atomic number 57 to 71 inclusive, either in hydrogen form (Zeolite Molecular Sieves Structure, Chemistry and Uses, DW BRECK, J.WILLEY and sons 1973).
• the supported catalyst comprises 0.01% to 25% by weight relative to the total weight of the NiO catalyst, preferably 0.1 to 10% by weight of NiO and 4.99% to 50% by weight relative to the total weight of the catalyst of WO 3 , preferably 9.99% to 40% by weight of WO 3 and 25 to 95% by weight of at least one acidic porous mineral matrix and preferably 50% to 90% by weight of said matrix.
• Said catalysts are advantageously analyzed by IR, NMR, and Raman spectroscopy and by elemental X-ray fluorescence analysis.
• the essential characteristics of the structures of formula (I) of the heteropolycomposed namely the position in counterion of nickel atoms in said heteropolycomposed and the degree of condensation, that is to say the amount of octahedra W in said heteropoly tungsten octahedra in the structure can be determined by 31 P NMR, 29 Si 1 11B and by Raman spectroscopy and X-ray fluorescence (XRF).
• Nuclear Magnetic Resonance is a spectroscopic technique for the structural analysis of molecules containing non-zero spin nuclei.
• the resonance frequency of the target nucleus will be directly affected by its chemical environment, so from a spectrum, it is possible to go back to the structure or by default to obtain partial information on the structure.
• the most commonly studied nuclei are 1 H, 13 C 1 14 N but NMR analysis can also be applied to 31 P, 29 Si, 1 1 B or 183 W nuclei.
• Raman spectroscopy is a non-destructive analysis technique that can determine molecular structures, study amorphous or crystalline systems and is particularly sensitive to small structures and therefore perfectly suited for the characterization of heteropolyanions.
• the distribution and location of the elements constituting the hydrogenating phase can be determined by techniques such as the Castaing microprobe (distribution profile of the various elements), Transmission Electron Microscopy coupled with an X analysis of the catalyst components (EDX), or else by establishing a distribution map of the elements present in the catalyst by electron microprobe. These techniques make it possible to demonstrate the presence of these exogenous elements added after the synthesis of the amorphous material with hierarchical and organized porosity comprising constituent silicon of the catalyst according to the invention. The distribution and location of tungsten, nickel and the group consisting of elements P, B and Si can be determined using these techniques.
• the overall composition of the catalyst according to the invention can be determined by Fluorescence X (FX) on the catalyst in the pulverulent state or by Atomic Absorption (AA) after acid attack of the catalyst.
• FX Fluorescence X
• AA Atomic Absorption
• Another subject of the invention relates to a process for the preparation of said heteropolycomposed consisting of a keggin lacunar type heteropolyanion nickel salt comprising in its tungsten structure the following steps: 1) synthesis of the keggin heteropolyanion containing tungsten of formula:
• Ba barium
• A is selected from phosphorus, silicon and boron
• W is tungsten
• O oxygen
• y 0 or 2
• Ba (OH) 2 barium hydroxide
• the tungsten-containing keggin heteropolyanion prepared according to step 1) is the heteropolyanion of formula: Ba x AW 11 O 39 , zH 2 O and the nickel salt of the heteropolyanion Keggin containing tungsten is the compound of the formula: Ni x AW 11 O 39 , zH 2 O.
• the keggin heteropolyanion containing tungsten prepared according to step 1) is the heteropolyanion of formula: Ba x + 1 AW 9 O 34 , zH 2 0 and nickel salt keggin heteropolyanion containing tungsten is the compound of the formula: Ni x + 1 AW 9 O 34 , zH 2 O.
• the heteropolytungstite acids H m AW 12 O 40 defined above are advantageously solubilized instantaneously in contact with water.
• the introduction of the basic compound barium hydroxide advantageously renders the solution less acidic and the tungsten octahedra of the initial heteropolytungstite acids decondensate to form the compounds AW 11 O 39 231 " or in which A respectively is phosphorus when the initial heteropolytungstite acid is H 3 PW 12 O 40 , wherein A is silicon when the initial heteropolytungstite acid is H 4 SiW 12 O 40 and wherein A is boron when the Initial heteropolytungstite acid is H 5 BW 12 O 40 .
• the heteropolyanionic structures are then advantageously surrounded by Ba 2+ ions to compensate for the negative charge.
• the compounds of formula (I 1 ) advantageously precipitate instantly or not depending on the concentration of the solution.
• the solution is then advantageously filtered and the compounds of formula (I 1 ) are advantageously isolated.
• step 2) of the process for preparing said heteropolycomposed compound according to the invention it is a question of substituting all the Ba 2+ cations with Ni 2+ cations so as to obtain the compound of formula (I) from the compound (I 1 ).
• the compounds of formula (I 1 ) are advantageously brought back into solution at the desired concentration.
• the ion exchange according to the 2nd step is a process by which the Ba 2+ ions in counterion position in the compounds of formula (I 1 ) and (II 1 ) in solution are advantageously removed from said solution by adsorption on the ion exchange resin to be replaced by an equivalent amount of other ions of the same charge emitted by said resin, here Ni 2+ cations.
• the ions of opposite charges here the anions of formula AW 11 O 39 2 * ' or AWgO 34 2 (x + 1) " (where A is phosphorus, silicon or boron) are not affected and said anionic structures of lacunary keggin type remain fully preserved.
• the ion exchange resin is advantageously finely divided, in order to present the maximum contact surface with the solution; it is therefore in the form of very fine grains that the ion exchange resins are used.
• the cation exchange resins used are acidic cation exchange resins, the functional groups of which are advantageously sulphonate anions -SO 3 ' , carboxylate -CO 2 " , aminodiacetate -N (CH 2 CO 2 ) 2 , phophonate -PO 3 2 " , or phosphinate> PO 2 " , etc.
• the strongly acidic sulfonic cation exchange resins are used.
• the resins are then advantageously in this case in the form of a polystyrene sulfonate crosslinked with divinylbenzene.
• These resins are advantageously chosen for their difference in affinities between the different cations which follows this order: H + ⁇ Na + ⁇ Ni 2+ ⁇ Ba 2+ .
• H + ⁇ Na + ⁇ Ni 2+ ⁇ Ba 2+ In general, it has been noted that when it is desired to increase the difference in affinity between several ions, for the same type of resins, it is necessary to increase the crosslinking of the resin.
• step 2) of said preparation process said cation exchange resins are previously exchanged with Ni 2+ cations.
• the first exchange reaction which will prepare the resin for the reaction of step 2 is advantageously written: 2R Na + + Ni 2+ ⁇ - (R) 2 Ni 2+ + 2 Na + in which R ' represents for example a sulphonate SO 3 'site
• the solution at the outlet of the ion exchange resin may then be advantageously used to directly impregnate at least one support formed of at least one acidic porous mineral matrix or may optionally undergo evaporation preferably to concentrate the solution.
• the catalysts supported according to the invention may then be prepared by any method known to those skilled in the art since the essential characteristics on the nickel position and the degree of condensation of the tungsten octahedra in the catalyst in the dried state are obtained.
• the catalysts supported according to the present invention are prepared in two stages.
• the first step consists in preparing the salt corresponding to the heteropolyanion referred to in formula (I) according to the process for preparing said heteropolycomposed consisting of a nickel salt of keggin-type heteropolyanions comprising in its structure the tungsten defined above and the second step is the impregnation on the support.
• the introduction of the heteropolyanion on Fe support to obtain a supported catalyst can therefore advantageously be done conventionally by any technique known to those skilled in the art before, during or after shaping the support.
• the introduction heteropolyanion on a support shaped by the well known technique of dry impregnation in which a) the support, for example a commercial aluminosilicate, is advantageously impregnated with an aqueous solution containing the desired amount of heteropolyanions and optionally molybdenum and / or tungsten introduced in another form and optionally another element of group VIII introduced in another form, b) the wet solid is advantageously allowed to stand under a humid atmosphere at a temperature between 10 and 80 0 C, c) the solid obtained in step b) is advantageously dried at reduced pressure or not at a temperature of between 50 and 300 ° C.
• step c) the solid obtained in step c) is calcined at a temperature of between 300 and 1000 0 C and more precisely between 300 and 550 0 C for a period of 1 to 24 hours and preferably for a period of 2 to 6 hours, under oxidizing atmosphere (pa for example air or oxygen), neutral (for example nitrogen or argon) or reducing (for example hydrogen).
• oxidizing atmosphere pa for example air or oxygen
• neutral for example nitrogen or argon
• reducing for example hydrogen
• the catalyst previously impregnated for the first time is then advantageously dried under the same conditions as previously described and optionally calcined under the same conditions as previously described. It is then advantageously impregnated a second time with an aqueous solution containing the heteropolyanions of formula (I) a second time. Multiple impregnations can be repeated as many times as necessary.
• the catalysts according to the invention can advantageously be manufactured and used in the form of powder, crushed compacted sieved powder, pellets, granules, tablets, rings, balls, wheels, spheres or extrudates. preferably in the form of sieved crushed compacted powder, spheres or extrudates. It is however advantageous that the catalyst is in the form of extrudates with a diameter of between 0.5 and 5 mm and more particularly between 0.7 and 2.5 mm.
• the shapes are cylindrical (which can be hollow or not), cylindrical twisted, multilobed (2, 3, 4 or 5 lobes for example), rings.
• the cylindrical shape is preferably used, but any other shape may be used.
• the present invention also relates to the use of said catalyst comprising said heteropolycomposed in a hydrocracking process, hydroconversion and / or hydrotreatment.
• the catalysts used in the field of hydrocracking are bifunctional catalysts combining an acid function (provided by the support) and a hydro-dehydrogenating function (provided by metal sulphides).
• the acid function participates in the isomerization and cracking reactions while the hydro-dehydrogenating function will participate in the actual hydrotreatment reactions that is to say I 1 HDN, I 1 HDS, and I 1 HDA (hydrodearomatization ).
• Any hydrocracking reaction begins with a step involving a hydrogenation reaction or a dehydrogenation reaction involving a hydro-dehydrogenating metal site.
• the first step of paraffin cracking thus begins with the generation of an olefin from a paraffin via a dehydrogenation reaction.
• the first step of cracking an aromatic nucleus begins with the hydrogenation of the aromatic ring because a benzene nucleus is more difficult to crack than the same hydrogenated nucleus.
• Vacuum distillate hydrocracking is a key process selectively leading to middle distillates (gas oil and kerosene) of excellent quality. It is the choice of the balance between the force and many of the acidic sites and the quality of the hydrogenating function which will determine the selectivity of the catalyst. Thus, a low crisp function with a strong hydrogenating function will make it possible to avoid successive crackings and will make it possible to be more selective in Middle Distillates. Comparatively, a strong cracking function with a low hydrogenating function will favor successive crackings and the generation of light cuts or even gas.
• the quality of the middle distillates cuts depends strongly on the hydro-dehydrogenating function and its ability to hydrogenate the aromatic rings and to increase the H / C ratio.
• the smoke point of kerosene (PF> 25mm) is in particular conditioned by a limiting aromatic content of not more than 20%.
• the cetane index of diesel (IC> 51) is also conditioned by a low aromatic content, otherwise the specification will not be achieved.
• the catalysts according to the invention are advantageously used for the treatment of hydrocarbon cuts, generally in the presence of hydrogen, at a temperature greater than 200 ° C., under a pressure greater than 1 MPa.
• the space velocity being between 0.1 and 20 h -1 and the amount of hydrogen introduced is such that the volume ratio by volume of hydrogen / liter of hydrocarbon is between 80 and 5000 l / l.
• the catalysts according to the invention are advantageously used for hydrocracking and / or hydroconversion of hydrocarbon cuts.
• the catalysts according to the invention can be used for the hydrotreatment of hydrocarbon feeds, alone or upstream of a hydrocracking / hydroconversion process.
• the catalysts according to the invention Prior to the injection of the feedstock, the catalysts according to the invention, either in the dried state or in the calcined state, are preferably subjected to a sulphidation treatment so as to obtain sulphide type catalysts, the treatment Sulfurization process making it possible, at least in part, to convert the metal species into sulphides before they come into contact with the feedstock to be treated
• This activation treatment by sulphurisation is well known to those skilled in the art and can be carried out by any method already described in the literature either in-situ, that is to say in the reactor, or ex-situ.
• the source of sulfur may advantageously be elemental sulfur, carbon disulfide, hydrogen sulphide, sulfur-containing hydrocarbons such as dimethylsulphide, dimethyl disulphide, mercaptans, thiophene compounds, thiols, polysulfides, such as, for example, ditertiononylpolysulfide or TPS-37 from the company ATOFINA, sulfur-rich petroleum cuts such as gasoline, kerosene, diesel, alone or in mixtures with one of the sulfur compounds mentioned above.
• the preferred source of sulfur is hydrogen sulphide or sulfur-containing hydrocarbons such as dimethyl disulphide.
• a conventional sulphurization method well known to those skilled in the art consists of heating in the presence of hydrogen sulphide (pure or for example under a stream of a hydrogen sulphide hydrogenated mixture) to a hydrogen sulphide. temperature between 150 and 800 0 C, preferably between 250 and 600 0 C, generally in a crossed-bed reaction zone.
• Fillers A wide variety of fillers can advantageously be treated by the processes according to the invention described above and generally they contain at least 20% by volume and often at least 80% by volume of compounds boiling above 340 ° C.
• the charge may advantageously be LCO (light cycle OII (light gas oils from a catalytic cracking unit)), atmospheric distillates, vacuum distillates, for example gas oils resulting from the direct distillation of the crude or conversion units such as that the
• FCC FCC, coker or visbreaking, as well as feeds from aromatics extraction units of lubricating oil bases or from solvent dewaxing of lubricating oil bases, or distillates from desulphurization processes or hydroconversion to fixed bed or bubbling bed of RAT (atmospheric residues) and / or
• the fillers have a boiling point T5 greater than 340 ° C., and more preferably greater than 370 ° C., ie 95% of the compounds present in the feed have a boiling point greater than 340 ° C. 0 C, and more preferably greater than 370 0 C.
• the nitrogen content of the feedstocks treated in the processes according to the invention is usually greater than 500 ppm, preferably of between 500 and 10,000 ppm by weight, more preferably between 700 and 4000 ppm by weight and even more preferably between 1000 and 4000 ppm.
• the sulfur content of the fillers treated in the processes according to the invention is usually between 0.01 and 5% by weight, preferably between 0.2 and 4% and even more preferably between 0.5 and 3%. .
• the charge may optionally advantageously contain metals.
• the cumulative nickel and vanadium content of the feeds treated in the processes according to the invention is preferably less than 1 ppm by weight.
• the asphaltene content is generally less than 3000 ppm, preferably less than 1000 ppm, even more preferably less than 200 ppm.
• Guard beds In the case where the feedstock contains resins and / or asphaltenes-type compounds, it is advantageous to precharge the feedstock on a bed of catalyst or adsorbent other than the hydrocracking or hydrotreatment catalyst. .
• the catalysts or guard beds used according to the invention are in the form of spheres or extrudates. It is however advantageous that the catalyst is in the form of extrudates with a diameter of between 0.5 and 5 mm and more particularly between 0.7 and 2.5 mm.
• the shapes are cylindrical (which can be hollow or not), cylindrical twisted, multilobed (2, 3, 4 or 5 lobes for example), rings.
• the cylindrical shape is preferably used, but any other shape may be used.
• the guard catalysts may, in another preferred embodiment, have more particular geometric shapes in order to increase their void fraction.
• the void fraction of these catalysts is between 0.2 and 0.75.
• Their outer diameter can vary between 1 and 35 mm.
• hollow cylinders hollow rings, Raschig rings, serrated hollow cylinders, crenellated hollow cylinders, pentaring carts, multi-hole cylinders ...
• These catalysts may have been impregnated with an active phase or not.
• the catalysts are impregnated with a hydro-dehydrogenation phase.
• the CoMo or NiMo phase is used.
• These catalysts may have macroporosity.
• the guard beds can be marketed by Norton- Saint-Gobain, for example the MacroTrap® guard beds. Guard beds can be marketed by Axens in the ACT family: ACT077, ACT935,
• the catalysts having the highest void content are preferably used in the first catalytic bed or first catalytic reactor inlet.
• the preferred guard beds according to the invention are HMC and I ⁇ CT961. Operating conditions
• the operating conditions such as temperature, pressure, hydrogen recycling rate, hourly space velocity, can be very variable depending on the nature of the load, the quality of the desired products and facilities available to the refiner.
• the hydrocracking / hydroconversion or hydrotreatment catalyst is advantageously generally brought into contact, in the presence of hydrogen, with the charges described above, at a temperature greater than 200 ° C., often between 250 and 480 ° C., advantageously between 320 ° C. and 320 ° C.
• the space velocity is between 0.1 and 2Oh 1 and preferably 0.1-6h, preferably 0.2-3h '1
• the amount of hydrogen introduced is such that the volume ratio liter of hydrogen / liter of hydrocarbon is between 80 and 5000I / I and most often between 100 and 2000 l / l.
• the hydrocracking and / or hydroconversion processes using the catalysts according to the invention cover the pressure and conversion ranges from mild hydrocracking to high pressure hydrocracking.
• Mild hydrocracking is understood to mean hydrocracking leading to moderate conversions, generally less than 40%, and operating at low pressure, generally between 2 MPa and 6 MPa.
• the catalyst of the present invention can advantageously be used alone, in one or more fixed bed catalytic beds, in one or more reactors, in a so-called one-step hydrocracking scheme, with or without liquid recycling of the unconverted fraction. , optionally in combination with a hydrorefining catalyst located upstream of the catalyst of the present invention.
• the catalyst of the present invention can advantageously be used alone, in one or more bubbling bed reactors, in a so-called one-step hydrocracking scheme, with or without liquid recycling of the unconverted fraction, optionally in in combination with a hydrorefining catalyst in a fixed bed or bubbling bed reactor upstream of the catalyst of the present invention.
• the bubbling bed operates with removal of spent catalyst and daily addition of new catalyst to maintain stable catalyst activity.
• the catalyst of the present invention can be used in one or both reactors in association or not with a catalyst hydrorefining process upstream of the catalyst of the present invention.
• the so-called hydrocracking in one step, comprises firstly and in a general manner advanced hydrorefining which aims to carry out a hydrodenitrogenation and a desulphurization of the charge before it is sent on the hydrocracking catalyst proper , especially in the case where it comprises a zeolite.
• This extensive hydrorefining of the feed leads only to a limited conversion of the feedstock into lighter fractions, which remains insufficient and must therefore be completed on the more active hydrocracking catalyst.
• no separation occurs between the two types of catalysts. All of the effluent at the outlet of the reactor is injected onto the hydrocracking catalyst proper and only then is separation of the products formed carried out.
• This version of the hydrocracking also called "Once Through" has a variant that has a recycling of the unconverted fraction to the reactor for further conversion of the charge.
• the silica content by weight of the support used in the composition of the catalyst is between 5 and 30% and preferably between 5 and 20%.
• the silica content by weight of the support used in the composition of the catalyst is between 20 and 80% and preferably between 30 and 60%.
• the catalyst according to the present invention is used upstream of a zeolitic hydrocracking catalyst, for example based on zeolite Y 1, it will be used advantageously a catalyst having a low weight of silica as defined above. It can also be advantageously used in combination with a hydrorefining catalyst, the latter being located upstream of the catalyst of the present invention.
• the conversion is generally (or preferably) less than 50% by weight and preferably less than 40%.
• the catalyst according to the invention may advantageously be used upstream or downstream of the zeolite catalyst. Downstream of the zeolite catalyst, it makes it possible to crack the polyaromatic hydrocarbons as described in particular in the book "Hydrocracking, Science and Technology” J.Scherzer, Editions M.Dekker Incorporated, 1996.
• the catalyst according to the invention can advantageously be used alone in one or more reactors. In the context of such a process, it will be possible to advantageously use several reactors in series, the bubbling-bed reactor (s) containing the catalyst according to the invention being preceded by one or more reactors containing at least one hydrorefining catalyst in bed. fixed or bubbling bed.
• the conversion of the fraction of the charge caused by this hydrorefining catalyst is generally (or preferably) less than 30% by weight and preferably less than 25%.
• the catalyst according to the present invention can also be used in a one-step hydrocracking process comprising a hydrorefining zone, an area allowing the partial elimination of ammonia, for example by a hot flash, and an area comprising a hydrocracking catalyst.
• This process for hydrocracking fillers one-stage hydrocarbon-based hydrocarbons for the production of middle distillates and optionally oil bases comprises at least a first reaction zone including hydrorefining, and at least a second reaction zone, in which the hydrocracking of at least a part of the reaction zone is carried out; effluent from the first reaction zone.
• This process also involves an incomplete separation of the ammonia from the effluent leaving the first zone. This separation is advantageously carried out by means of an intermediate hot flash.
• the hydrocracking performed in the second reaction zone is carried out in the presence of ammonia in an amount less than the amount present in the feed, preferably less than 1500 ppm by weight, more preferably less than 1000 ppm by weight and even more preferably lower. at 800 ppm weight of nitrogen.
• the catalyst of the present invention is preferably used in the hydrocracking reaction zone in association or not with a hydrorefining catalyst located upstream of the catalyst of the present invention.
• the catalyst according to the invention can be used upstream or downstream of the zeolite catalyst. Downstream of the zeolite catalyst, it makes it possible in particular to convert polyaromatic hydrocarbons or polyaromatic hydrocarbon precursors.
• the catalyst according to the invention can advantageously be used either in the first reaction zone in pretreatment converting, alone or in combination with a conventional hydrorefining catalyst, situated upstream of the catalyst according to the invention, in one or more catalytic beds, in one or more reactors.
• the catalyst according to the invention may advantageously be used in a hydrocracking process comprising: a first hydrorefining reaction zone in which the feedstock is brought into contact with at least one hydrorefining catalyst having in the standard activity test a cyclohexane conversion rate of less than 10% by weight. a second hydrocracking reaction zone in which at least a portion of the effluent resulting from the hydrorefining stage is brought into contact with at least one zeolitic hydrocracking catalyst having in the standard activity test a conversion of cyclohexane greater than 10% by weight, the catalyst according to the invention being present in at least one of the two reaction zones.
• the proportion of the catalytic volume of hydrorefining catalyst generally represents 20 to 45% of the total catalytic volume.
• the effluent from the first reaction zone is at least partly, preferably completely, introduced into the second reaction zone of said process.
• An intermediate separation of the gases can be carried out as previously described
• the effluent leaving the second reaction zone is subjected to a so-called final separation (for example by atmospheric distillation optionally followed by vacuum distillation), so as to separate the gases.
• a so-called final separation for example by atmospheric distillation optionally followed by vacuum distillation
• the conversion into products having boiling points below 340 ° C., or even below 370 ° C., is at least 50% by weight.
• Two-stage hydrocracking comprises a first stage whose objective, as in the "one stage” process, is to perform the hydrorefining of the feedstock, but also to achieve a conversion of this feedstock. order in general from 40 to 60%.
• the effluent from the first step then undergoes separation (distillation), which is often called intermediate separation, which aims to separate the conversion products from the unconverted fraction.
• separation distillation
• intermediate separation which aims to separate the conversion products from the unconverted fraction.
• the second step of a two-stage hydrocracking process only the fraction of the unconverted feedstock in the first step is processed. This separation allows a two-stage hydrocracking process to be more selective in middle distillate (kerosene + diesel) than a one-step process.
• the intermediate separation of the conversion products avoids their "over-cracking" in naphtha and gas in the second step on the hydrocracking catalyst.
• the unconverted fraction of the feedstock treated in the second stage generally contains very low levels of NH 3 as well as organic nitrogen compounds, generally less than 20 ppm by weight or less than 10 ppm. weight.
• the same configuration of fixed bed or bubbling bed catalytic beds can be used in the first step of a so-called two-stage scheme, whether the catalyst is used alone or in combination with a conventional hydrorefining catalyst.
• the catalyst according to the invention can be used upstream or downstream of the zeolite catalyst. Downstream of the zeolite catalyst, it makes it possible in particular to convert polyaromatic hydrocarbons or polyaromatic hydrocarbon precursors.
• Molybdenum and cobalt are dry co-impregnated in an aqueous medium on a cogel-synthesized commercial silica-alumina support (380 m 2 / g).
• the precursor salt of tungsten is ammonium metatungstate (NhU) 6 H 2 W 12 O 40 , 4H 2 O
• the precursor salt of nickel is nickel nitrate Ni (NO 3 J 2 , 6H 2 O.
• the precursor of silicon is supplied in the form of rhodorsil
• the silicas coming from the support are, of course, not taken into account in this calculation.
• the extrudates are dried at 120 ° C. overnight and then calcined under 450 air.
• Molybdenum and cobalt are dry co-impregnated in an aqueous medium on a cogel-synthesized commercial silica-alumina support (380 m 2 / g).
• the precursor salt of tungsten is ammonium metatungstate (NH 4 J 6 H 2 W 12 O 40, 4H 2 O 1 precursor salt of nickel is nickel nitrate Ni (NO 3) 2 .6H 2 O, the precursor of P is H 3 PO 4.
• the extrudates are dried at 120 ° C. overnight, then calcined in air at 450 ° C. for 2 hours.
• the content of tungsten oxide is 16.7%
• the nickel oxide content is 1.7%
• the P 2 O 5 content is 0.5%; which corresponds to a real NL ⁇ / V ratio of 0.32 atoms / atoms and a P / W ratio of 0.1.
• This catalyst B is representative of an industrial catalyst and is not in accordance with the invention.
• the concentration of the solubilized salt is 0.1 mol.l -1, the solution thus prepared then passes over a cation exchange resin, the solution is added dropwise and this resin is a strongly acidic commercial resin. uniform particle size distribution at 585 ⁇ m tower: Dowex Marathon C.
• the backbone is made of styrene gel cross-linked by DVB.
• the functional groups are SO 3 ' sulfonates. It is received conditioned in Na + form.
• the resin Prior to the exchange of Ba 2+ by Ni 2+ , the resin is packaged in Ni 2+ form with a saturated solution of NiSO 4 . Once the resin packaged in Ni 2+ form, 92 ml of resin is placed in a stainless steel column of 10 mm internal radius. The bed height is then 450 mm.
• This column is placed in an oven heated to 45 ° C to allow the solubilization of salts during the exchange step.
• the 170 ml of solution heated to 45 ° C pass over the column.
• 160 ml of solution containing Ni 4 SiW 11 O 39 is recovered at a concentration of 0.1 mol. L "1.
• the solution is then partially evaporated and concentrated.
• the final concentration of Ni 4 SiW 11 O 39 in the solution is 0.16 mol. the 1.
• the 50.4 g of Ba 7 Z 2 PW 11 O 39 product are redissolved in 160 ml of deionized water and heated slightly to 45 ° C to solubilize the barium salt of the heteropolyanion. The concentration of solubilized salt is then 0.1 mol. The 1 .
• the solution thus prepared then passes over a cation exchange resin. The addition of the solution is done drop by drop.
• This resin is a strongly acidic commercial resin with a uniform particle size distribution around 585 ⁇ m: Dowex Marathon C.
• the backbone is made of a styrene gel crosslinked by DVB.
• the functional groups are SO 3 ' sulfonates. It is received conditioned in Na + form.
• the resin Prior to the exchange of Ba 2+ by Ni 2+ , the resin is packaged in Ni 2+ form with a saturated solution of NiSO 4 . Once the resin packaged in the Ni 2+ form, 75 ml of resin are placed in a stainless steel column 10 mm in internal radius. The bed height is then 369 mm. This column is placed in an oven heated to 45 ° C to allow the solubilization of salts during the exchange step. The 160 ml of solution heated to 45 ° C pass over the column. Once the first 41 milliliters of solution corresponding to the dead volume are passed, 150 ml of solution containing Ni 7Z 2 PW 11 O 39 is recovered at a concentration of 0.1 mol. L "1. The species Ba 7Z2 PW 11 O 39 is present on the scale of trace.
• FIGS. 1 and 2 show the impregnating solutions containing respectively Ni 4 SiW 11 O 39 and Ni 7Z 2 PW 11 O 39 prepared in Examples 3 and 4 analyzed by 29 Si NMR in the case of Example 3 and by 31 P NMR in the case The spectra are shown respectively in FIGS. 1 and 2.
• FIG. 1 shows the 29 Si NMR spectrum of the solution containing Ni 4 SiW 11 O 39 .
• Figure 2 shows the 31 P NMR spectrum of the solution containing Ni 7Z 2 PW 11 O 39 .
• the catalysts prepared in Examples 3 and 4 were characterized in the dried state by Raman spectroscopy.
• Table 1 groups together the main bands and characteristics of the terminal bonds WO of the heteropolyanions. These bands with a wavenumber of less than 1000 cm -1 are characteristic of lacunar heteropolycomposites.
• Weak-based keggin type HPA's of Examples 3 and 4 have wave numbers of 1011 cm -1 and 1000 cm -1, respectively .
• the aim of the hydrogenation test of toluene in the presence of aniline is to evaluate the hydrogenating activity of the supported or bulk sulfurized catalysts in the presence of H 2 S and under hydrogen pressure.
• the isomerization which characterizes the acid function of the catalyst is inhibited by the presence of aniline, at low temperature and / or by the presence of NH 3 (resulting from the decomposition of aniline) at a higher temperature.
• Aniline and / or NH 3 will react via an acid-base reaction with the acidic sites of the support. The isomerization reactions characteristic of the acidity of the support are then non-existent.
• the catalytic test is carried out in the gas phase, in a fixed bed reactor through.
• the test is broken down into two distinct phases, sulphidation and catalytic testing.
• the test is performed at 60 bar.
• the catalysts are sulphurized in situ dynamically in a fixed bed tubular reactor through a pilot unit type catatest (manufacturer Vinci Technologies), the fluids flowing from top to bottom.
• the hydrogenation activity measurements are carried out immediately after sulphurization under pressure without re-airing with the hydrocarbon feedstock which was used to sulphurize the catalysts.
• the sulfurization charge is the same as that of the test.
• the test load is composed of dimethyl disulphide (DMDS), toluene, cyclohexane and aniline.
• DMDS dimethyl disulphide
• the stabilized catalytic activities of equal volumes of catalysts (4 cm 3 ) and at a temperature of 350 ° C. are measured.
• the catalytic performances are collated in Table 2. They are expressed in relative activity, while that of catalyst B is equal to 100.
• Table 2 shows the significant hydrogenating power gain obtained on the catalysts prepared from the heteropoly compounds Ni 4 SiW 11 O 39 and Ni 7Z 2 PW 11 O 39 according to the invention (catalysts T1 and T2 respectively) relative to the catalysts which are their formulation homologs but which are prepared by conventional routes, not using kggin-type heteropolyanion-containing Ni salts containing W.
• EXAMPLE 7 Evaluation of the CI, C2, C3 and C4 Catalysts in Hydrocracking of a Previously High Vacuum Vacuum Distillate at High Pressure.
• Catalysts A, B, T1 and T2 whose preparations are described in Examples 1, 2, 3, 4 are used under the conditions of the hydrocracking of vacuum distillates at high pressure (14 MPa).
• the feed used is a hydrotreated feed.
• a scheme is simulated in which a hydrotreatment catalyst is in sequence with the catalysts A, B 1 T1 and T2
• the catalytic test unit comprises a fixed bed reactor with upflow flow.
• 40 ml of catalyst according to the invention (A, B, T1, T2) are introduced.
• the catalyst undergoes an in situ sulphurization step before reaction.
• the catalyst is sulfurized to 14 MPa, 350 ⁇ C by means of a direct distillation gas oil supplemented with 2% by weight of DMDS. Once the sulfurization is complete, the charge described above can be transformed.
• CN 370 0 C is equal to:
• CN 370 0 C [(% of 370 ° C ⁇ ⁇ "i u nt s) - (% of 370 ° C “ charg ⁇ )] / [100 - (% of 370 0 C " chatB ⁇ )] with
• SB DM 1 The gross selectivity of middle distillates (150-370 ° C. cut) 1 denoted SB DM 1 is taken as:
• SB DM [(fraction at 150 - 370 effl uents)] / [(% of 370 ° C " ⁇ ffi ue nts)] •
• the catalytic performances are expressed by the required temperature to reach 60% net conversion to products having a boiling point below 370 0 C and by the crude selectivity of middle distillates (150-370 ° C. cut). Conversion and selectivity are expressed from simulated distillation results.
• the preceding examples thus show the whole point of using a catalyst according to the invention (T1, T2) to carry out the hydrocracking of hydrocarbon feeds.
• the catalysts according to the invention make it possible to obtain higher conversions of the feed without loss of selectivity in middle distillates.
• the improved hydrogenating power of the active phase through the use of new W-containing keggin-type heteropolyanion Ni salt structures allows to hydrogenate more aromatic rings and thus generate more crackable and cracked molecules, so a larger conversion.
• the hydrogenating function is stronger, the molecules are less overcooled, less gasoline and gas are generated, which increases the selectivity in middle distillates.

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